Gd ZEOLITE AND HYDROCARBON CONVERSION PROCESS WITH Gd ZEOLITE CATALYST

ABSTRACT

A process for converting hydrocarbons comprises contacting a hydrocarbonaceous feed in a conversion zone at an elevated temperature with a substantially anhydrous Gd alumino-silicate zeolite and recovering an upgraded hydrocarbon conversion product. The process can be used to obtain a product having a significantly greater average molecular weight than that of the hydrocarbonaceous feed. the preferred zeolite is crystalline, capable of adsorbing benzene, and, in the hydrated condition, is chemically characterized by the empirical formula Mx(ALO2)x(SiO2)y.(H2O)z, where x, y and z are integers, the ratio x:y being usually from 1.0 to 0.2 and where at least 25 percent (and more preferably more than 40 percent) of the negative charge associated with the aluminum of the alumino-silicate framework is satisfied by a cation of Gd or a cation of an oxide or a hydroxide of Gd. The Gd alumino-silicate catalyst is especially useful for conversions involving the liquid phase catalytic contacting of C2-C9 olefin in admixture with C4-C6 isoparaffin to obtain liquid paraffin alkylate for gasoline blending. The catalyst is also useful for the polymerization (in liquid or vapor phase) of olefins, particularly to produce liquid polyolefins which can be converted, as by hydrogenation, to paraffins in the gasoline boiling range.

United States Patent [72] lnventors Francis William Kirsch Wayne; David S. Barmby, Media; John D. Potts, Springfield, all of Pa. [21] Appl. No. 715,998 [22] Filed Mar. 26, 1968 [45] Patented Nov. 30, 1971 [73] Assignee Sun Oil Company Philadelphia, Pa.

Continuation-impart of application Ser. No. 581,129, Aug. 25, 1966, now abandoned. This application Mar. 26, 1968, Ser. No.

[54] GD ZEOLITE AND HYDROCARBON CONVERSION PROCESS WlTH GD ZEOLITE CATALYST 11 Claims, No Drawings Primary Examiner-Herbert Levine Attorneys-George L. Church, Donald R. Johnson, Wilmer E.

McCorquodale,Jr. and Barry A. Bisson ABSTRACT: A process for converting hydrocarbons comprises contacting a hydrocarbonaceous feed in a conversion zone at an elevated temperature with a substantially anhydrous Gd alumino-silicate zeolite and recovering an upgraded hydrocarbon conversion product. The process can be used to obtain a product having a significantly greater average molecular weight than that of the hydrocarbonaceous feed. the preferred zeolite is crystalline, capable of adsorbing benzene, and, in the hydrated condition, is chemically characterized by the empirical formula M,(ALO ),(SiO ),,'(H O),, where x, y and z are integers, the ratio x:y being usually from 1.0 to 0.2 and where at least 25 percent (and more preferably more than 40 percent) of the negative charge associated with the aluminum of the alumino-silicate framework is satisfied by a cation of Gd or a cation of an oxide or a hydroxide of Gd. The Gd alumino-silicate catalyst is especially useful for conversions involving the liquid phase catalytic contacting of C C olefin in admixture with C,C isoparaffin to obtain liquid paraffin alkylate for gasoline blending. The catalyst is also useful for the polymerization (in liquid or vapor phase) of olefins, particularly to produce liquid polyolefins which can be converted, as by hydrogenation, to parafi'ms in the gasoline boiling range.

GD ZEOLITE AND HYDROCARBON CONVERSION PROCESS WITH GD ZEOLITE CATALYST CROSS-REFERENCE TO RELA'I'ED'APPLICA'I'TONS This application is a continuation-in-part of copending 'application Ser. No. 581,129, filed Aug. 25, 1966 which is now abandoned.

Gd-containing zeolites which can be utilized as catalysts in the subject process have been describedincopending application Ser. No. 590,225, filed Oct. 28, 1966 of Ronald D. Bushick entitled "Alumino-Silicate Catalyzed Reactions of Polycyclic Aromatic Hydrocarbons" and in copending application Ser. No. 581,129, filed Aug. 25, 1966 of Francis William Kirsch, David S. Barrnby and John D. Potts entitled Process for Paraffin-lefin Alkylation" and in copending appiication, Ser. No. 716,!90, filed of even date with the present application, of Francis William Kirsch, David S. Barmby and John D. Potts entitled Process for Parafiin-Olefin Alkylation and in copending application Ser. No. 718,980, filed of even date with the present application, of Ronald D. Bushick entitled "Combination of Gd Alumino-Silicate Catalyst and Hydrogenation Catalyst," and in copending application Ser. 'No. 715,994, filed of even datewith the present application of Alfred E. l-lirschler entitled Hydrocarbon Conversion Process with Gd Catalyst," all of these being-assigned to the Sun Oil Company. The disclosure of all of the above-cited applications is hereby incorporated in the present application. In addition to the above-referred to applications, the following later filed copending applications, assigned to the Sun Oil Company, are related to the disclosure of the present application and contain a specific reference incorporating this disclosure therein:

Process for producing gasoline blending components, Kirsch-Barrnby-Potts.

BACKGROUND OF THE INVENTION Although it is known to utilize crystalline alumino-silicate zeolites containing cations of lanthanum, cerium or of certain rare earth salt mixtures as hydrocarbon conversion catalysts e.g., see U.S. Pat. No. 3,140,249 and U.S. Pat. No. 3,2l0,267), the art has failed to realize that incorporation of substantial quantities of gadolinium cations in an amorphous or crystalline alumino-silicate zeolite can be used to produce an adsorbant for aromatic hydrocarbons or a catalyst which is especially useful for hydrocarbon conversion reactions, and particularly conversions involving carbonium-ion mechanisms. Similarly, the art has failed to appreciate that a combination of a Gd alumino-silicate catalyst with a hydrogenation catalyst can be especially useful for conversions involving catalytic contacting of hydrocarbons in the presence of hydrogen, such as aromatization of naphthenes or olefins, cyclizations, reforming, hydrocracking and hydroisomerization.

BRIEF SUMMARY OF THE INVENTION Hydrocarbon conversion reactions, such as cracking, dehydrogenation, reforming, alkylation, dealkylation, cyclization and isomerization can be effected by contacting a hydrocarbon feed with a catalyst comprising an alumino-sil- IOIORZI 0539 ieate zeolite containing cations of gadolinium, such as Gd, Gd(Ol-I)*, and Gd(OH),". Also efiective as catalysts in such processes are novel catalysts comprising gadolinium-containing zeolites which also contain magnesium cations, aluminum cations, silver cations, nickel cations, zinc cations, cerium cations, lanthanum cations, cations of the hydroxides or oxides of these metals or mixtures of two or more of such cations.

The preferred zeolite catalyst is crystalline and capable of adsorbing benzene, has an atomic ratio Al/Si of 0.65 to 0.35 and contains at least one Gd(OH), cation for every eight atoms of aluminum in the alumina-silicate framework. The zeolite can also be utilized as an adsorbent, as for separating aromatic hydrocarbons from less polar compounds. In conversions involving oxidative regeneration of this catalyst (or adsorbant), crystallinity can decrease, usually accompanied by a decrease in activity and/or selectivity. The resulting, more amorphous, zeolite can be effective as a catalyst, particularly at conversion temperatures which are greater than those required for the corresponding conversion with an equal weight of crystalline zeolite.

An especially useful hydrocarbon conversion reaction is the hydroisomerization of the C -C paraffin hydrocarbons which are capable of conversion to more highly branched isomers, in order to obtain a more highly branched product with improved octane ratings. Another especially useful conversion is the alkylation of C C,, aromatic (or C -C alkyl aromatic) hydrocarbons, or C -C paraffin hydrocarbons,

'with olefin hydrocarbons. Another especially useful conver- FURTHER DESCRIPTION OF THE INVENTION Pentene-isomerization activity is a measure of the acid activity of a catalyst, and, therefore, indicative of the ability of the'catalyst to catalyze typical carbonium-ion reactions such as cracking, dealkylation, aromatic alkylation, polymerization, isomerization, etc. By utilizing the isomerization of pentene-l as a test reaction, it has been found that a substantially anhydrous GdI-IY catalyst, prepared by activation of a crystalline GdNH,Y zeolite (obtained by Gd-cation exchange of highly ammonium-exchanged sodium Y zeolite), is more effective than a similarly prepared Cel-IY catalyst wherein, instead of aqueous gadolinium cations, aqueous cerium cations were present in the exchange medium.

In the Gd aluminosilicate catalyst, at least 25 percent and, preferably, at least 40 percent of the electronegativity associated with the alumina-silicate framework is satisfied by cations of gadolinium or of its oxides or hydroxides, When the Gd catalyst contains less than one alkali metal cation (e.g. Na) for every four aluminum atoms in the alumino-silicate framework, the catalyst is especially useful for such hydrocarbon conversion reactions as isomerizing polycyclic aromatic hydrocarbons, paraffin-olefin alkylation and the cracking of gas oil. Preferably, the alumino-silicate zeolite is crystalline and is chemically characterized by the empirical formula M,.(AlO, ,(SiO,),-(l-l,0),, where x, y and z are integers, the ratio x/y being from 1.0 to 0.2 and where M is chosen from at least one of the following groups:

I. at least one Gd cation for every l2 atoms of aluminum in the alumino-silicate framework of said zeolite;

2. at least one cation of Gd( OH for every eight atoms of aluminum in the alumino-silicate framework of said zeolite;

3. at least one cation of Gd(Ol-i), for every four atoms of aluminum in the alumino-silicate framework of said zeolite;

4. a combination of the members of at least two of the above groups;

and wherein the balance of the cations necessary for electronic equivalency comprises l-l or cations of metals, metal oxides or metal hydroxides and wherein there is less than one alkali metal cation for every four atoms of aluminum in the alumino'silicate zeolite, more preferably, less than one alkali metal cation for every 10 atoms of aluminum preferably, when said zeolite is analyzed by ignitionatl,800 F., from 0.5 to 6 molecules of water is obtained for each atom of Gd in said zeolite.

The Gd zeolite can contain a such additional cations, the cations of magnesium, aluminum, silver, nickel, zinc, cerium, lanthanum and mixtures of these cations. In such catalysts it is preferred that at least one such cation is present for every 20 atoms of aluminum in the alumino-silicate framework of said zeolite. I

For most hydrocarbon conversions, the ratio x/y in the empirical formula of the zeolite should be in the range of 0.25 to 2. lfexcess water is present, the zeolite should be activated" by heating according to the procedure disclosedin' the aforementioned applications of Kirsch, Barmby and Potts. If the zeolite is deficient in fbound" water, water can be added, as by exposure to steam in air or nitrogen.

As used herein, the term framework," in reference to the alumino-silicate portion of the zeolite (which can be crystalline or amorphous), excludes those aluminum ions which are in exchange positions and which are neutralizing some of the negative charge associated with the aluminum atoms in the alumino-silicate tetrahedra of the zeolite. Note that aluminum in the alumino-silicate framework can be either trigonal or tetrahedral.

For such reactions as reforming, aromatization, hydrogen transfer, hyrocracking and hydroisomerization, it is preferred that the catalyst have incorporated therewith from 0.05 to 25 percent (more preferably, 0.05 to 5 percent) of a hydrogenation catalyst component containing a hydrogen-active metal such as platinum, palladium, rhodium, rhenium, ruthenium, molybdenum, cobalt or nickel (or a chemical compound, as an oxide or sulfide, of such a metal). The hydrogen-active metal can also be incorporated on a carrier (as alpha-alumina, microporous silica, conventional amorphous silica-alumina cracking catalyst, or acid-exchanged clays, such as montmorillonites or kaolin). When the hydrogen-active metal component (or a chemical compound of the metal) is so incorporated on a carrier, it is preferred that the Gd catalyst be physically admixed therewith.

When the hydrocarbon conversion involves cyclization and/or aromatization, as with a feed of n-pentene, n-hexene, n-heptene or 1,4-dimethylnaphthalene, the cyclization conditions comprise a temperature in the range of 350-850 F. and a pressure in the range of -750 p.s.i.g., preferably with the reactants maintained in the vapor or trickle phase. For aromatization and/or cyclization of a cracked naphtha, temperature in the range of 240-600 F. is preferred at atmospheric pressure. For a hydrogen transfer reaction, to produce aromatics from naphthenes, a temperature in the range of 300-500 F. at atmospheric pressure is preferred, as when cyclohexane and propylene are the feed hydrocarbons and the products are benzene plus propane.

For double-bond isomerization, such as for the conversion of 2-ethyll -butene to cis and trans 3-methyl-2-pentene, or the conversion of pentene-l to pentene-2, a temperature in the range of 70-400 F. and pressures from 0-75 p.s.i.g. are preferred, with the lower temperatures and higher pressures most preferred in order to reduce cracking.

For isomerization and/or transalkylation of alkyl benzenes, such as converting meta-xylene to ortho and para xylene, the hydrocarbon reactant can be either in liquid or vapor phase at a temperature in the range above about 60 C. and below cracking temperature. The preferred temperature range for xylene isomerization is l50-350 C. and preferably in the presence of added hydrogen (e.g. 5-75 p.s.i.

When the primary conversion reaction is cracking, a temperature in the range of 800l,l00 F. is preferred for a gas oil feed, preferably at atmospheric or slightly elevated pres- IOIOBIZ: 05

sure, although pressures as low as 1 mm. Hg and as high as 1,200 p.s.i.g. can be utilized in such cracking reactions. When the predominant reaction is hydrocracking, our preferred hydrogen-active metal is selected from Group Vlb, VIII, and more preferably comprises Ni, Pd or Pt. The preferred hydrogen pressures is in the range of 500-5 .000 p.s.i. at conversion temperatures from 650-l, 1 00 F.

For paraffin-olefin alkylation, the preferred process conditions with a C C, feed olefin are those of the aforementioned patent applications of Kirsch, Barmby and Potts. Generally, these involve a. contacting C C, monoolefin with C,-C isoparatfin and with a substantially anhydrous Gd zeolite catalyst at a temperature below the critical temperature of the lowest boiling hydrocarbon reactant and at a pressure such that each of the reactants is in liquid phase, and,

b. stopping such contacting after substantial alkylation has occurred but before the weight rate of production of unsaturated hydrocarbon becomes greater than the weight rate of production of saturated hydrocarbon.

Preferably, the feed olefin and feed paraffin are admixed prior to contact with the catalyst and the concentration of unreacted olefin is kept sufficiently low that predominantly saturated paraflin-olefin alkylation products are obtained rather than unsaturated products. This concentration is preferably less than 7, more preferably less than 12 mole percent, based on the total paraffin content of the reaction mixture. Also preferred is the use of a halide adjuvant (as HCl, CCl, and the C -C, monochloro paraffins) containing bromine, chlorine or fluorine, to increase the yield of liquid paraffin based on the olefin charged. Also preferred is a temperature in the range of 25-l20b C. and a mean residence time of the reaction mixture with the catalyst in the range of 0.05 to 0.5 hours per (gram of catalyst per gram of hydrocarbon in the reaction mixture). When the feed olefin comprises ethylene, conditions shown in U.S. Pat. No. 3,251,902 can be used to produce a liquid product; however, this liquid product is generally less preferred as a component of gasoline than are the highly branched liquid paraflin hydrocarbons which are produced by the aforementioned process of the Kirsch, Barmby and Potts applications.

For the isomerization of such polycyclic aromatic hydrocarbons as s-OHA to its isomer S-OHP, or S-OHP to its isomer s- OHA, the preferred conditions include a temperature above C. and below cracking temperature and are shown in the aforementioned application of Ronald D. Bushick, Ser. No. 590,225. This Bushick application also shows the preparation of a novel composition comprising an acidic Gd alumino-silicate catalyst and from 0.5 to 5 percent of a hydrogenation catalyst. Preferably the hydrogenation catalyst is selected from. the group consisting of platinum, palladium, nickel, nickel oxide, nickel sulfide, molybdenum oxide, molybdenum I sulfide, cobalt oxide, palladium oxide and mixtures thereof. The hydrogenation catalyst can be physically admixed with the acidic alumino-silicate, or have been incorporated into the alumino-silicate by salt impregnation or by ion exchange. When the salt has been introduced into the alumino-silicate catalyst by ion exchange, it is preferred that the hydrogenation catalyst be reduced, as with hydrogen, prior to contact of the catalyst with the hydrocarbon feed. Also preferred is a process for the isomerization of polycyclic aromatic hydrocarbons, such as s-OHA or s-OHP, wherein the Gd catalyst/ hydrogenation catalyst combination and from 25-1 ,000 p.s.i.g. of hydrogen are present in the reactor. The added hydrogen aids in maintaining the activity of the isomerization catalyst combination, and can be recycled at rates up to l0,000 s.c.f./bbl. of feed. The LHSV is preferably in the range of 0.255.0 volumes of feed per volume of catalyst per hour.

In any of the above-listed reactions, if the catalyst activity appreciably decreases during the course of the reaction, the catalyst may be separated from the hydrocarbon reactants and regenerated, as by burning in air. After such burning, water can be added to the catalyst, as by exposure to steam in air or nitrogen. When a hydrogen-active metal is incorporated into the zeolite catalyst, it is sometimes advantageous to reduce the regenerated combination with hydrogen, preferably at 250- 800 F prior to introduction of the hydrocarbonaeeous feed.

When the primary hydrocarbon conversion is a hydroisomerization or a reforming reaction, the preferred conditions inelude a hydrogen pressure of at least 25 p.s.i.g. and temperatures from 500700 F., although the conversion can be effected in the range of 2251,000 F., at total pressures in the range of 0-5,000 p.s.i.g. and hydrogenpressures in the range of 0.54,000 p.s.i.g. For the hydroisornerization of C -C paraffins, the preferred catalyst combination will contain from 0.1 to 2 percent of Pt, Pd or Re (or a mixture thereof) or from 1 to 10 percent of Ni.

Typical feeds and reaction conditions which are effective when utilizing the Gd catalyst, particularly when combined with a hydrogenation catalyst, for hydroisomerization or reforming are those in the following US. Pat. Nos. 2,834,439; 2,970,968; 2,971,904; 2,983,670; 3,114,695; 3,122,494; 3,132,089; 3,140,253; 3,146,279; 3,190,939; 3,197,398; 3,201,356; and 3,236,762.

In processes utilizing the Gd catalyst whether alone or in combination with a hydrogenation catalyst, halide adjuvants containing chlorine, fluorine or bromine can frequently be used to increase the degree of conversion. Preferred adjuvants include CC 1 l-lCl, AlBr BF HF and the C,-C chlorohydrocarbons.

ILLUSTRATIVE EXAMPLES 1n the following examples, example I shows the preparation of a preferred embodiment of the Gd catalyst and example 11 shows the incorporation therewith of a Pt-hydrogenation catalyst. Example 111 shows contacting n-pentane with this combination of a Gd catalyst and a Pt catalyst and obtaining, as the major product, isopentane. Example 1V shows a similar hydrocarbon conversion of n-pentane, wherein example 111 is repeated except that a Col-[Y zeolite is substituted for Gdl-lY zeolite in the catalyst combination. Example V shows a test reaction with a pentene-l feed which indicates that the Gd zeolite catalyst of example 1 has appreciably greater activity than a similar Ce zeolite catalyst for carbonium-ion reactions such as cracking (including gas oil cracking), example Vl shows the hydroisomerization of a straight run gasoline stream, by contacting with the Gd catalyst/hydrogenation catalyst combination of example 11, to upgrade the octane rating of the gasoline. Example Vll shows paraffin-olefin alkylation with the Gd zeolite catalyst of example 1.

EXAMPLE 1 About 500 g. of NaY zeolite was exchanged, filtered and washed for 16 cycles with aqueous NH CI utilizing the procedures disclosed in the aforementioned US. application, Ser. No. 581,129. The resulting Nl-LY zeolite was similarly exchanged for 16 cycles with aqueous gadolinium nitrate. The resulting Gd-exchanged NIL-exchanged zeolite was washed free of nitrate and unexehanged gadolinium ions, with distilled water, and dried in an oven at about 120 to produce a GdNH,Y zeolite. The zeolite was activated by heating slowly to 400 C. to remove water and decompose the bulk of any remaining ammonium ions. This activation utilized the procedures disclosed in the aforementioned U.S. Ser. No. 581,129. The zeolite before activation had the analysis listed in the attached table 1 under the heading Run No. 628 (Run No. 674 is also this zeolite). The resulting substantially an-' hydrous Gdl-lY zeolite was crystalline and capable of adsorbing benzene. The weight loss upon ignition analysis at l,800 C., of the activated zeolite was 3.41 percent.

EXAMPLE 11 A solution of Pt(l\ll-l ),C1 in water was added dropwise with stirring to a dilute aqueous suspension of the catalyst in water, at 55 C. The amount of PKNHQ CI used was rorosszs equivalent to 0.5 percent Pt in the activated catalyst. After the Pt salt addition was complete (about 1 hr.), the solution was stirred at 55 C. for 30 minutes, filtered, and the catalyst washed with distilled water until the washings were free of chloride ion. The catalyst was dried, heated to 400 C. in a stream of dry air and then reduced at 400 C. in the reactor in a flowing stream of H for one hour.

EXAMPLE lll N-pentane was passed through a bed of the activated catalyst combination of example 1, at a liquid hourly space velocity of 4.0 at 325 C./662 F. and 400 p.s.i.g., along with one mole of hydrogen for each mole of hydrocarbon feed. The product of this contacting contained 55.6 mole percent of isopentane. No more than 2 mole percent of the product was of lower molecular weight than the feed (thus, indicating a low degree of cracking) and less than 0.5 mole percent of the feed were products having a molecular weight higher than n-pentane.

EXAMPLE 1V Example 11 was repeated except that the catalyst combination was a similarly activated combination of an activated cerium-exchanged, ammonium-exchanged Y zeolite and 0.5 percent of Pt. The reaction product contained only 51.7 percent of isopentane. That is, the Gd zeolite catalyst combination produced nearly 8 percent more isopentane than did the Ce zeolite catalyst combination.

EXAMPLE V A 4.2 m1. portion of a solution of 21 percent pentene-l in npentane was shaken with 0.50 g. of each above catalyst. Portions of the liquid were removed periodically for analysis. After 7 minutes contact time the conversion to pentene-Z was 12.7 percent over the CeHY and 72.8 percent over the GdHY. The monomeric olefin concentrations in the liquid phase were 17.3 percent and 12.5 percent respectively, showing that the Grill! was more active for polymerization of the olefin as well as for the isomerization to pentene-2.

EXAMPLE VI A straight run gasoline feed was contacted at 325 C., 400 p.s.i.g. total pressure, in a tubular reactor, in the presence of added percent hydrogen, with a bed of the reduced catalyst combination of example 11. Table 1, under the heading GdHY 0.5 percent Pt" reports the analysis and calculated octane ratings of the product obtained from three such runs, at various space rates and hydrogen/hydrocarbon ratios. These data indicate that preferred conditions for such gasoline upgrading (of streams containing at least 25 percent C,,C normal paraffin) with a Gd zeolite-hydrogenation catalyst combination (at 300-340 C.) include an LHSV of 1 to 4 (more preferably 1.5 to 2.5) at a hydrogen to hydrocarbon molar ratio in the range of 1 to 6.

TABLE 1 (Isomerizatlon o1 Cr-Ce gasoline for octane upgrading all runs at 325 C. and 400 p.s.lrg.

Product (HEY-+0.15% Pt Hydrocarbon, wt. percent Feed A B 1 C a O; 0. 6 0. 6 0. 8 0. 3 2. 4 1. 9 2.3 4. 6 4. 2 4. 2 4. 6 1.8. 7 35. 2 33. 2 31. 9 35.8 22. 4 21. 5 21. 7 1. 1 4. 4 5. 5 5. 5 3. 5 3. 0 3. 0 3. 0 2. 2 2. 7 3.0 3.0 13. 6 10. 4 11. 3 11. 4 6. 1 7. 2 7. 7 7. 8 1i. 4 t1. 5 7. 0 7. 0 1. 7 0.11 1. 0 0. 9 0. 2 0. 1 0. 1 0. 1 0.7 Heptanes. 0. 5 Trace Trace Trace Octanes 1.2

3 .fi 1. same zeolite but by activation in helium rather than in air 1%: Z213 Z213 (Run 674). Also shown are similar runs made with catalysts t prepared by air activation of a highly ammonium-exchanged i i-. fiiiitiiiiiiiijj::::::::: 533* 3335 32:? 55:3 Type Y Mme (Run 576), a Prepared as in example! 1 RunAan BLHSV an HIHC but exchanged with aqueous cerium nitrate instead of the a mm B at LHSV and HIHC: 7 aqueous gadolinium nitrate (Run 642)-and a zeollte prepared h 'fi q 3 2332 33 fi s/28 by such cerium exchange of a highly ammonium-exchanged nirsv u uld hourly spe r e el city in volume or feed per volume of YP X (Run cataiyst per our. Ie claim:

48 how! CJ400 9- 3 lo 1. AGd alumino-silicate zeolite which is chemically charac- LI ISV with n-pentane prior to contact with the straight run gaso ine. grind y the empirical formula M,(Al0,),(SiO,),'(l-I,O),, where x, y and z are integers, the

EXAMPLE v" ratio x/y being from 0.65 to 0.2 and where M is chosen from at least one of the following groups:

This example illustrates the use of substantially anhydrous a. at least one Gd cation for every 12 atoms of aluminum acidic crystalline Gd alumino-eilicate zeolite as a paraflinin the alumino-silicate framework of said zeolite;

olefin alkylation catalyst. The catalyst of example I (prepared b. at least one cation of Gd(OH)"* for every eight atoms of by activating a l6-cycle Gd /l6-cycle Nl-lf-exchanged Type aluminum in the alumino-silicate framework of said Y zeolite) was charged in amount of 23.3 g. into a l-liter, zeolite;

stirred autoclave containing a four-member baffle to diminish c. at least one cation of Gd(Ol-l),* for every four atoms of vortex formation. Then 444 milliliters of liquid isobutane and aluminum in the alumina-silicate framework of said 1.0 g. of tertiary butyl chloride was added. The stirring rate (of zeglite; gr 7 MM g TABLE 2.LIQUID PHASE ISOPARAFFIN OLEFIN ALKYLATION WITH SOL ID ZEOLITE CATALYSTS Gadolinium versus Ammonium versus Cerium and Type X versus Type Y Zeolite [Autogenous pressure, 80 C., i-C|-ane/C4-ene-2=15 (min), 3.67 hr., 1.0 g. tertiary butyl chloride edjuvant] Catalyst:

Zeolite before activation GdNH Y GdNH4Y N HIY CeNH4X' CeNHiY Activation (400 C.) Gas--. Air He Air Air Air Run No 628 674 596 622 60 Or paraflin yield, wt. percent 00 163. 0 169. 8 43. 5 130. 0 161.6 05+ unsaturates, wt. percent 00 0.00 0.05 0. 2 0.0 0. 00 05+ paraffin distribution, mole percent:

88. 1 88. 2 59. 3 85. 7 85. 9 ll. 9 11. 8 38. 7 14. 2 l4. 1 0. 0 0.0 2. 0 0. 1 0. 0

27. 4 28. 4 13. 6 15. 5 24.4 5. 9 5. 4 5. 1 4. 1 5. 6 28. 8 29. 1 39. 6 34. 0 32.0 2 3,3- 37. 9 37. 1 41. 7 46. 4' 38. 0 Catalyst analysis (ignited basis, before activatlon):

Wt. percent Na 9. 97 Wt. percent:

Ce Gd 14. 39 Wt. percent N 1.09 Wt. percent loss on ignition 26. Analysis of base Na zeolite (before exchange,

ignited basis):

Wt. percent Na 9. 51 Wt. percent A1203. 16. 56 Wt. percent SiO 29 Wt. percent 108.15; ighiii 241212 Base CeNHi X zeolite analyzed 37.56% S10; (17.56% 81).

a six-member, flat-blade turbine) was adjusted such that subd. a combination of the members of at least two of the above stantially all of the zeolite was suspended in the liquid isobugroups;

tam? (about 550 -P-m). The temperature in the reactor was and wherein the balance of the cations necessary for elecraised to 80 C. using suflicient nitrogen to produce a t tal tronic equivalency of the zeolite comprise H or cations of pressure of 250 p.s.i.g. Under these conditions, nearly all of metals, metal oxides or metal hydroxides and wherein there is the hydrocarbon is in the liquid phase. Then a liquid mixture 60 less than one alkali metal cation for every four atoms of aluof one part by volume of butene-2 and 5 volumes of isobutane minum in the alumino-silicate portion of said zeolite, and was charged from a Jerguson gauge via a needle valve and dip wherein when said zeolite is analyzed by ignition at L800 F tube into the isobutane-catalyst slurry (and near the bottom of from 0.5 to 6 molecules of water is obtained for each atom of the reactor) at the rate of one milliliter of mixture per minute Gd in said zeolite, said zeolite being useful as a catalyst for for a period of 220 minutes. Nearly all of the hydrocarbon was hydrocarbon conversion reactions.

maintained in liquid phase. At the end of this time the reaction 2. The zeolite of claim 1 wherein said zeolite is at least 50 was stopped by cooling the reactor to l7 C., then separating percent crystalline, said crystalline portion being capable of the reaction mixture from the catalyst by first removing the adsorbing benzene, and wherein at least 40 percent of the normally gaseous hydrocarbons at room temperature and atelectronegativity associated with the aluminum of said mospheric pressure, and then separating the liquid product framework is satisfied by a cation containing gadolinium or by from the catalyst py filtration. Some propane and n-butane but a combination of cations containing gadolinium and cerium no methane, ethane, ethylene or propylene were found in the wherein the gadolinium cations comprise at least 60 percent normally gaseous hydrocarbons. Table 2 reports the composiof the charge associated with said combination.

tion of the C, liquid product of this reaction (Run 628) and 3. Zeolite according to claim 1 wherein said zeolite is o M .rsasiiqafi l shaseta t rermssilrenth c y a lin and p e o ing be e e. has n o ic ratio Al/ Si of 0.65 to and contains at least one Gd(Ol-i),* o

cation for every eight atoms of aluminum in the alumino-silicate framework.

4. Zeolite according to claim 1 wherein said alumino-silicate zeolite has an X-ray diffraction pattern which evidences at least some degree of crystaliinity and wherein the atomic ratio Al/Si of the alumina-silicate framework of said crystalline portion of said zeolite is from 0.65 to 0.35.

5. Zeolite according to claim 1 wherein the ratio x]: is from 0.25 to 2 and wherein the atomic ratio Al/Si of the aluminosilicate framework of said crystalline portion of said zeolite is from 0.65 to 0.35.

6. A hydrocarbon alkylation process comprising contacting C,C, olefin with C C, isoparaffin or C,C aromatic hydrocarbon at an elevated conversion temperature with a Gd alumina-silicate zeolite according to claim 1 and recovering an upgraded hydrocarbon alkylation product.

7. Process according to claim 6 wherein said alumino-silicate zeolite is at least 50 percent crystalline and wherein at least one C -C olefin is contacted with C C isoparafl'in and said product contains an appreciable quantity of C liquid paraffin.

8. Process according to claim 7 wherein the atomic ratio Al/Si of the alumino-silieate framework of said crystalline portion ofsaid zeolite is from 0.65 to 0.35.

9. Process according to claim 7 wherein the ratio xzz in the empirical formula of said substantially anhydrous Gd aluminosilicate zeolite is in the range of 0.25 to 2.

10. Process according to claim 7 wherein at least 40 percent of the negative electrical charge associated with the aluminosilicate framework is satisfied by at least one cation from the group consisting of Gd, Gd( OH and Gd( OH 11. A hydrocarbon alkylation process comprising contacting C,-C, olefin with C.C isoparaffin or C, C,, aromatic hydrocarbon at an elevated conversion temperature with a Gd alumino-silicate zeolite according to claim 2 and recovering an upgraded hydrocarbon alkylation product.

i i i i t 

2. The zeolite of claim 1 wherein said zeolite is at least 50 percent crystalline, said crystalline portion being capable of adsorbing benzene, and wherein at least 40 percent of the electronegativity associated with the aluminum of said framework is satisfied by a cation containing gadolinium or by a combination of cations containing gadolinium and cerium wherein the gadolinium cations comprise at least 60 percent of the charge associated with said combination.
 3. Zeolite according to claim 1 wherein said zeolite is crystalline and capable of adsorbing benzene, has an atomic ratio Al/Si of 0.65 to 0.35 and contains at least one Gd(OH)2 cation for every eight atoms of aluminum in the alumino-silicate framework.
 4. Zeolite according to claim 1 wherein said alumino-silicate zeolite has an X-ray diffraction pattern which evidences at least some degree of crystallinity and wherein the atomic ratio Al/Si of the alumino-silicate framework of said crystalline portion of said zeolite is from 0.65 to 0.35.
 5. Zeolite according to claim 1 wherein the ratio x/z is from 0.25 to 2 and wherein the atomic ratio Al/Si of the alumino-silicate framework of said crystalline portion of said zeolite is from 0.65 to 0.35.
 6. A hydrocarbon alkylation process comprising contacting C2-C9 olefin with C4-C6 isoparaffin or C6-C22 aromatic hydrocarbon at an elevated conversion temperature with a Gd alumino-silicate zeolite according to claim 1 and recovering an upgraded hydrocarbon alkylation product.
 7. Process according to claim 6 wherein said alumino-silicate zeolite is at least 50 percent crystalline and wherein at least one C2-C9 olefin is contacted with C4-C6 isoparaffin and said product contains an appreciable quantity of C5 liquid paraffin.
 8. Process according to claim 7 wherein the atomic ratio Al/Si of the alumino-silicate framework of said crystalline portion of said zeolite is from 0.65 to 0.35.
 9. Process according to claim 7 wherein the ratio x:z in the empirical formula of said substantially anhydrous Gd alumino-silicate zeolite is in the range of 0.25 to
 2. 10. Process according to claim 7 wherein at least 40 percent of the negative electrical charge associated with the alumino-silicate framework is satisfied by at least one cation from the group consisting of Gd 3, Gd(OH) 2 and Gd(OH)2
 1. 11. A hydrocarbon alkylation process comprising contacting C2-C9 olefin with C4-C6 isoparaffin or C6 -C22 aromatic hydrocarbon at an elevated conversion temperature with a Gd alumino-silicate zeolite according to claim 2 and recovering an upgraded hydrocarbon alkylation product. 